Conversion of hydrocarbons



Nov. 11, 1947. R. F. RUTHRUFF CONVERSION OT HYDROCARBONS Filed Dec. 13, 1944 4 Sheets-Sheet 1 v 6 77/36 MINUTES F/ GUAEI wmmww k .UQQOQK KO k zwbkwnx 4 6 TIME MINU TE 5 0 0 0 0 W 0 6 5 4 3 Z I k UBQOKQ Ls RRWUQPMR 7 H Um m A M Q 0 B R Now 11, 1947. R. F. RUTHRUFF 2,430,784

CONVERSION OF HYDROC'ARBQNS Filed Dec. 13, "1944 4 Sheets-Sheet 2 TL'BlA/D EKGEAIERATOZ Eeacfor je aarazor INVENTO ,4. M

ATTORNEY NOV. 11, 1947. 4 RUTHRUFF 2,430,784

CONVERSION OF HYDHOCARBONS Filed Dec. '13, 1944 4 Sheets-Sheet 3 FIG. L17

Eegenera for feparafbr fi lma BY ATTORNEY Nov. 11, 1947. F. RUTHRUFF 2,430,784 I CONVERSION 0F HYDROCARBONS I 4 Sheets-Sheet 4 Filed Dec. 1s,"'1944 NOT f w M WR Rm Ev N. m F. 8 v 0 a Y E m xukfiw xk ATTORNEY Pla ed Nov. 11, 1941 2,430,784

UNITED STATES PATENT OFFICE CONVERSION OF HYDROCARBONS Robert F. Ruthrufl, Chicago, Ill., assignor to The M. W. Kellogg Company, Jersey City, N. J., a corporation of Delaware Application December 13, 1944, Serial No. 567,907

Claims. 1

The present invention relates to the conversion of hydrocarbons, particularly the conversion of high-boiling hydrocarbons to low-boiling hydrocarbons and is a continuation in part of my copending application Serial No. 277,885, filed June 7, 1939, issued March 20, 1945, as Patent No. More specifically, my invention relates to the conversion in the presence of a catalyst or contact agent of high-boiling hydrocarbon mixtures such as petroleum crudes or heavy fractions thereof to low-boiling fractions such as gasoline.

It has been common practice to convert highboiling hydrocarbons to low-boiling hydrocarbons by thermal decomposition or thermal cracking, and this art as applied to hydrocarbons is well known and highly developed.

By subjecting hydrocarbons to elevated temperature, decomposition or cracking sets in with the production of various conversion products. When, for example, a mixture of liquid hydrocarbons boilingin the temperature range 400-750 F., is thermally cracked or decomposed, the followin conversion products are obtained: gas, gasoline, cycle stock having approximately the same boiling range as the hydrocarbon charge, tar and coke. conversion zone, gas, gasoline, tar and coke are obtained as ultimate conversion products. Usually, gasoline is the desired decomposition product while gas, tar and coke are, under most circumstances, undesirable.

Many advantages follow the use of contact materials or catalysts in the decomposition or crackingof hydrocarbons. For example, the operating temperature required for a given amount of conversion may be considerably lowered in comparison with the temperatures required in operations conducted in the absence of catalysts. Additionally, the quality of the gasoline produced in the tion may be considered equivalent to part of the tar produced in thermal cracking.

While the catalytic conversion of hydrocarbons is superior to thermal processes, the former operation is not perfect for here too, undesirable products (gas and coke) are formed. By the practice of this invention the production of these unde- By returning the cycle stock to theslrable products is decreased, while the production of gasoline is increased.

the deposited coke at a suitable temperature. A, great variety of catalytic materials, differing widely in physical structure and chemical composition have been suggested for use as cracking catalysts, and in each instance, these materials have been recognized as requiring periodic regeneration treatments for removal of. deposited carbonaceous material in order to enable them to be employed for repeated conversion treatments.

The basis of this invention resides in the observation and discovery that, the alumina-silica type of cracking catalyst exhibits certain distinctive phenomena during the initial portion of the conversion cycle with respect to the products produced, and in the provision of a process arising from this observation whereby amore favorable distribution and enhanced yield of the desired conversion products are obtained.

The catalytic material suitable for use in the practice of the invention comprises either naturally occurring or synthetically prepared mixtures or compounds of silica and alumina, suitably prepared so as to exhibit a high degree of catalytic cracking activity. A variety of different methods for the preparation of catalysts of this type have been described heretofore in the art. For example, a suitable type of alumina-silica cracking catalyst for use in accordance with my invention may be artificially prepared by impregnating a hydrogel of silica with a heat-decomposable salt of alumina such as aluminum nitrate, and then heating the impregnated hydrogel to decompose themitrate, thereby producing a suitable cracking catalyst consisting of a hard porous silica gel impregnated with alumina, this method of preparation being that described in U. S. Patent 1,782,857. Other materials containing a1 mine. and silica such as naturally occurring, or activated adsorbent clay materials such as for example fullers earthand bentonite, having the eifect of catalytically converting the higher boiling hydrocarbons into lower ones, may be employed. An activated bleaching clay sold under the trade name, Super- Filtrol? is particularly suitable for use in accordance with my invention. This product is pro duced by the conversion of certain types of raw bentonites into highl active adsorbent products by intimately contacting the ground raw clay with mineral acid under suitable conditions and thereafter removing the products of reaction by successive washings with large volumes of hot water. After de-watering, the pulp is dried under carefully controlled conditions followed by final grinding to desired mesh specification.

The term "alumina-silica cracking catalyst as employed herein and in the appended claims, designates and is limited to a well recognized class of materials known for their capability of catalyzing the conversion of high-boiling hydrocarbons to lower boiling hydrocarbons within the gasoline boiling range characterized by both high yield and quality of the gasoline produced. This catalytic conversion is further characterized by the continuous conversion during the catalytic contact of a portion of the charge to produce a carbonaceous deposit on the catalyst. Activated clays such as "Super-Filtrol and synthetic composites including silica gel and alumina are well known examples of this class of catalyst material. Other materials such as pumice, although including alumina and silica in some form, are known to lack catalytic activity of the character referred to and are, therefore, expressly excluded from the term "alumina-silica cracking catalyst.

The procedure employed in the practice of my invention, and its various features and advantages will be apparent from the following detailed description thereof, given in connection with the appended drawings, wherein:

Figures I and II are graphical representations of the per cent production, based on the hydrocarbon charged, of the various products of oncethrough catalytic cracking over alumina-silica type of cracking catalysts, as a function of the catalyst exposure time; and

Figures III, IV and V, each illustrates diagrammatically a suitable type of apparatus for the practice of specific embodiments of the invention.

Referring to'Figures I and II, the curves shown are graphicalrepresentations of the instantaneous yields or the per cent production, relative to feed stock, of the conversion products produced by passage of the feed in a once-through operation over alumina-silica type of crackin catalysts as a function of the catalyst exposure or contact time. Referring to the individual curves, curve A, represents coke yield; B, yield of gaseous material; C, yield of cycle stock; and D, yield of gasoline.

It is to be noted that the yields shown arenot cumulative, but rather represent the instantaneous yields obtained during any given period of catalyst life. For example, the yield data shown at ten minutes represent the roduction of conversion prcducts obtaining at the instant when the reactor containing the catalyst has been onstream ten minutes, and not the cumulative yield over the first ten minutes of the conversion cycle. The specific data shown in Figure I were obtained when passing West Texas gas oil over a catalyst consisting Of an acid treated clay of the Super- Filtrol" type. A temperature of 850 F. was employed and the charge. was passed at a rate of 0.3 liquid volume per volume of catalyst per hour.

The results in Figure I show that when using this catalyst, initially no gasoline or cycle stock is formed, only large amounts of coke and gas. As time on-stream increases, the yields of gas and coke both decrease rapidly, the yield of cycle stock increases slowly while gasoline production rapidly increases to an optimum and th n more slowly declines.

The following explanation is suggested to cover the behavior exhibited but it is to be understood that this is theory only, and in no Way limits the scope of the invention. It is believed that the contact material charged to the reactor is not of itself the true cracking catalyst but that it is a material capable of producing carbon or carbonaceous residues of peculiar orientation and properties and that it is this carbon or these residues that form the true cracking catalyst. During the first few minutes on-stream the major product formed is this oriented carbon which is of course deposited on the catalyst. As time goes on, production of gasoline increases rapidly, reaching a maximum in the present instance at an on-stream period of approximately ten minutes. At this time, coke production is practically nil while gas production is very low. When the on-stream period is increased beyond ten minutes, the proportion of gasoline in the reaction product decreases with increasing rapidity. It is believed that initially the contact material has little or no ability to make gasoline. As carbon is deposited on the surfaces of this contact material, this carbon, due to its peculiar orientation and properties which are due to the natur of the surface of the contact material upon which it is deposited, has the' ability to convert the charge to gasoline. Conversion to gasoline increases rapidly as the contact material become covered with carbon; likewise as the contact material becomes covered with carbon, less charge becomes converted to carbon. However, as cracking progresses, it is believed that tar or pitch forms as a by-product and this material also is deposited on the contact agent, covering the active carbon already thereon. The tar or pitch or carbonaceous material derived therefrom does not, it is believed, possess the required orientation necessary for converting gas oil to gasoline and accordingly gasoline production decreases. As this occurs, the yield of cycle stock increases simultaneously since there is no fresh surface of contact material to convert it to coke and no orientated carbonaceous material to convert it to gasoline. Apparently the contact material during any one cycle acquires a double layer. When fresh, the contact material gives largely coke and gas; when covered with oriented carbon it produces gasoline; and when the carbon is covered with tar or decomposition products thereof. the whole is inactive both as a carbon producer and as a gasoline producer.

Figure II is similar to Figure I except that Figure II represents conditions wherein the gas oil charge was passed over the alumina-silica catalyst at a rate of 1.0 liquid volume per volume of catalyst per hour. The time on-stream yield relationships in the two figures are quite similar, an differences being explainable on the basis Of the different charging rates. In Figure I, maximum gasoline yield was 73%, attained when the catalyst was on-stream 10.5 minutes. In Figure II, gasoline yield was maximum at 52.5% when the on-stream period was 2.7 minutes, approximately. The lower gasoline yield in this case reflects the shorter contact time. It will be noted that the increase in gasoline yield to the maximum is faster in Figure II than in Figure I, while the decline from the maximum is slower. This last is due to the slower rate at which the oriented carbon surface is blanketed with tar or pitch and reflects in turn the lower extent of cracking at the higher charge rate. It appears, however, that the rate of depositing active, oriented carbon on the contact material is not so much a function of contact time as it is of the total amount of charge passed. For example, in Figure II, maximum activity was reached in 2.7 minutes. This multiplied by the charge rate, gives 2.? volumes of charge passed to reach maximum activity. In Figure I, maximum activity was reached in 10.5 minutes and this multiplied by the charge rate 0.3, gives 3.15 volumes of charge passed to reach maximum activity. Within the limit of experimental accuracy, these two values are substantially identical.

It may be observed from Figures I and II that for any length of cycle X, the gasoline yield could be increased if the initial period could be, in effect, eliminated. In addition, not only is the gasoline yield increased but also the gasoline to gas plus coke ratio is very substantially increased. More specifically, in Figure I, if the reaction is conducted over the period 6 to minutes shown, the gasoline yield is higher than over the period,

'0 to 9 minutes, and the gasoline "tosgas plus coke ratio is much higher. Likewise, in Figure II, the yield of gasoline and the product distribution is much more favorable over the period, 2 to 6 minutes than the period, 0 to 4 minutes.

It may be further observed that when conducting a catalytic conversion operation in accordance with the operating conditions obtaining for Figure I, if the products are sent to waste durin the initial period, for example, the first five minutes of the reaction cycle after which the conversion products are collected for use in the production of distillate boiling within the usual gasoline boiling range, theproduct distribution in the finally collected products is much improved. However, under such conditions no useful result has been attained since the initial product showing poor distribution was sent to waste.

In accordance with my invention the initial period of the cycle characterized by undesirable product distribution and yield is, in effect, eliminated by subjecting the catalyst to a preconditioning treatment prior to the conversion reaction. In accordance with this treatment, a quantity of carbonaceous material is formed or deposited on the particular type of alumina-silica cracking catalyst employed approximating the quantity normally deposited during said initial period above described. The quantity of carbon to be thus formed will, in general, range in quantity from about 0.5% to 2.0%, by weight, of the catalyst, and preferably resides in the somewhat narrower range of about 0.8% to 1.5%. Preconditioning of the catalyst, in accordance with my invention, may be effected by the decomposition of a hydrocarbon mixture which is readily broken down or decomposed to produce a mixture of carbon and other hydrocarbons by a suitable decomposition treatment, and contacting the decomposition products with the fresh or regenerated alumina-silica catalyst in such manner that carbon is deposited thereon to the required extent. Preferably, the conditioning treatment is effected by passing the hydrocarbons selected for the treatment, in contact with the fresh or regenerated catalyst under reacting conditions variety of types of catalytic reactors and regeneration equipment. One type involves the socalled static bed" type of operation wherein the catalyst is disposed in the reactor in the form of a stationary or static bed through which the hydrocarbons undergoing treatment are passed. Upon substantial deactivation'of the catalyst, the flow of hydrocarbons thereover is discontinued, and a regenerating gas such as air is passed over the spent catalyst to burn off deposited carbon. Usually a plurality of such catalyst reactor chambers are arranged in parallel and suitably manifolded with respect to the incoming stream of treated hydrocarbons and regenerating gas, so that the operation is substantially continuous,

,one reactor being on-stream while another is being regenerated. Accordingly, a complete cycle in a given reactor involves both a conversion period and a regeneration period. In accordance with my invention the complete cycle includes an additional conditioning period. A suitable apparatus for the practice of this embodiment of the invention is shown in Figure III.

Referring to Figure III, a single reactor I1 is shown, partly in elevation and partly in section. Charging stock, which may consist of reduced crude or heavy gas oilis passed by line I and pump 2 to furnace 3. "The preheated charge enters separator 4, through line 5, overhead products passing through line 6 and through opened valve 28 to a reactor or reactors (similar to IT, hence not shown) which are exercising the cracking function, valve 1 in line 8 being closed. Heavy products in the preheated charge accumulate in the bottom of separator 4 from whence they may be eliminated from the system if desired through valve 9 in line l0. Alternatively, these heavy products may be passed through valve ll ifold I4 is provided with a plurality of branched pipes 20, one or more for each tray. If desired, an atomizlng fluid, suitably preheated, such as steam, gas made in the process or from another source, flue gas made in the regeneration process or-from an outside source, may be passed through line 2| to manifold 22, said manifold having a plurality of branched pipes 23, each side pipe corresponding to a side pipe 20 from manifold 14.

The heavy charge is distributed to a series of atomizers or sprays 24 by means of the plurality of side pipes 20. Preferably the atomizers or sprays 24 are disposed in the layers of catalyst l8 on the perforated trays l9 although they may also be disposed above the catalyst. Also, it is adapted to decompose it to a mixture of hydrocarbons and carbon, the latter forming the required deposit of activating carbon on the catalyst. The quantity of carbon thus deposited is 1, dependent on the quantity of the selected hydronot necessary to have atomizers or sprays 24 in or near each tray of catalyst. While this arrangement is preferable, satisfactory results can be obtained by atomizing, vaporizing or spraying all of the heavy charge in the bottom of reactor H. The atomizing, vaporizing or spraying of the heavy charge may be aided by the introduction of fluid through line 2|.

In operating the above described apparatus to secure the benefits of this invention, the heavy portion of the charge obtained from the bottom of separator 4 is passed over the freshly regenerated hot catalyst in reactor I 1, and is decomposed thereby formingthe desired carbon deposit on the catalyst, while the lighter portions of the charge pass through line 6 to another reactor (not shown) which is on the cracking cycle. Passage of the heavy portion of the charge through line l4 and decomposition thereof is continued until the desired amount of carbon is deposited on the catalyst.

Vaporizable products derived by the decomposition of the heavy portion of the charge leave reactor I! through opened valve 25 in line 26, and may be disposed of as desired. After a short preconditioning treatment, valve 21 in manifold I 4, valve 25 in line 26, valve 31 in line 2|, and valve 28 in line 6, are closed while valve 1 in line B is opened, light product from the top of separator 4 then passing over the preconditioned catalyst in reactor ll, the resulting prodnot then being sent to conventional fractionating or condensing means (not shown) through opened valve 29 in line 30. Also, at this stage,

valve 15 i opened and the conditioning stock passed through line l6 to a reactor ready for the conditioning treatment, a continuous operation being thus assured.

Because of the heavy nature of the conditioning stock it is readily decomposed into carbon and other hydrocarbons, and the time required for accomplishing the conditioning treatment is very short. For example, when operating under the conditions described in connection with Figure I, a period of about 2.5 minutes brings the catalyst to a condition similar to that shown by the catalyst after minutes (Figure I) where a relatively light gas oil was used as charge. In

one series of experiments, satisfactor results have been obtained by passing preheated charge to the separator 4 at a rate of 100 volumes in unit time, separating it into 80 volumes of overhead and 20 of bottoms, pumping these bottoms at a rate of 20 volumes in unit time through line I4 for a time of 2.5 minutes which constitutes the conditioning period, and then passing the overhead from separator 4 to the reactor I! at a rate of 80 volumes per unit of time for a time of 10 minutes which constitutes the conversion or cracking period of the cycle.

If desired; the product withdrawn through line 26 during the conditioning treatment may be recycled in the conditioning operation, for example by introducing this material through line 3| and valve 32. Alternatively, other conditioning materials may be added to the system through line 3| in addition to, or replacing in whole or part material from .line I2. Suitable materials for such purposes include non-volatile hydrocarbons such as petroleum pitch, coal tar pitch, wax introduced as such or dissolved in a suitable volatile solvent such as naphtha. These materials may be suitably preheated if desired but it should be borne in mind that these are contacted with the catalyst in reactor l1 immediately after the regeneration step under which conditions the catalyst may be considerably above reaction temperature so that the addition of conditioning feed at relatively low temperatures may be necessary or desirable to aid in bringing the catalyst temperature down to the required operating temperature before the conversion or cracking cycle begins. For this reason, in some cases it is necessary to cool the heavy bottoms from separator 4 before using them as a conditioning means.

It is apparent that when using a light charging stock containing little or not bottoms suitable for conditioning, conditioning materials from outside sources must be used. For convenience,

stocks suitable for use in the conditioning of catalysts may be termed carbogens.

At the conclusion of the cracking cycle in which'the preconditioned catalyst, prepared as previously described, is employed the regeneration cycle begins. Valve I in line 8 is closed as is valve 29 in line 30. Revivification gas enters through valve 33 in line 34 and leaves by valve 35 in line 36. It is apparent that one complete cycle is divided into three portions (a) preconditioning (b) cracking and (c) regeneration.

My invention may be further employed in conjunction with the so-called moving-bed" type of catalytic cracking operation. In this type of operation, the catalyst is moved through the conversion zone during the conversion period of the cycle, and regenerated in a zone external of the conversion zone. Figure IV illustrates a suitable apparatus and flow procedure for use in the practice of this embodiment of the invention. Referring to Figure IV, the charge, such as reduced crude or heavy gas oil is introduced by line 4| and pump 42 to furnace 43. The preheated oharge enters separator 44 by means of line 45, overhead from said separator 44 passing to reactor 46 through line 41. The contact material or catalyst in reactor 46 is constantly moving downward, contact material being added through conveyor 48 and leaving through conveyor 49. Converted or cracked hydrocarbons leave reactor 46 through line 50, passing to conventional fractionating means or condensing means (not shown) as desired. Suitable feeding means or solids pumps 5| are provided at the top and bottom of reactor 46 for introducing and withdrawing the solid catalyst without substantial escape of vapor therefrom.

Spent catalyst leaving reactor 46 through conveyor 49 is regenerated in any suitable manner, one suitable form of regenerator being illustrated. This regenerator 52 contains a plurality of hearths 53, 54, 55, 56 and 51, each provided with one or more rakes 58 attached to rotatable shaft 59. Spent catalyst falls on the top hearth 53 and is distributed and agitated by means of the rake or rakes 58 which move over the surface of said hearth. The catalyst on hearth 53 is gradually moved down through the regenerator, resting in turn on hearths 54,55, 56 and 51 and is finally discharged into conveyor 48 and moved to the top of reactor 46 to repeat the cycle.

Means are provided for contacting the catalyst in regenerator 52 with air or dilute air. For example, air or dilute air may pass through duct 60 to ducts 6|, over the hearths 53, 54 and 55 and out through ducts 62 and duct 63. The regenerating fluid may be suitably warmed or cooled before entering duct 60 and part or all of the flue gas leaving 63 ma be recycled after eliminating a portion which is replaced by makeup air.

A separate duct 64 is shown supplying hearth 56. Inert material such as oxygen-free flue gas is supplied to duct 64 and may suitably be flue gas from duct 63. This inert flue gas is supplied at such a rate that it forms a seal, the inert mate rial forming a partition between hearth 56.and hearth 55. While catalyst can fall from the upper hearth 55 onto hearth 56 and then hearth 51,

' are passed through valve I in line 61, pump 68 and line 69 to sprayers or atomizers I8 in the immediate vicinity of hearth 51. As in the case of the process flow of Figure III, the hot regenerated catalyst at this stage may be at an elevated temperature considerably above the reaction temperature in zone 46. The sprayers or atomizers may suitably form the teeth of the rakes passing over hearth 51. If desired, steam,

flue gas, or gaseous hydrocarbons may be employed to aid in the vaporization, spraying or atomization of the heavy material from the bottom of separator 44. This may be added through line II. The products from hearth 51 may be removed through line I2 and worked up as desired. By this processthe catalyst is conditioned in the last hearth. i

The conditioning treatment may be effected, wholly or partly, at other points in the cycle if desired. For example, heavy oil may be vaporized, atomized or sprayed into conveyor 48 at one or more points or it may be vaporized, sprayed or atomized into the upper portions of reactor 46 through oil and steam inlet lines 6911 and Ila, similar to lines 69 and 'II.

As in the embodiment previouslydescribed, the heavy oil used in conditioning may be supplemented or replaced by material from sources other than the charge and where the charge is comparatively light, such outside sources, preferably, are employed. Conditioning oil from said outside sources may enterthe cycle through line 13 and valve 14.

It will be noted that the reactor shown in Figure IV, differs from that shown in Figure III in that, with the former, operations are continuous. While the catalyst in reactor 46 differs in activity from top to bottom of said reactor, the integrated activity of all the material in reactor 46 is always constant regardless of the length of time the reactor has been on-stream. Accordingly, the processed charge leaving reactor 46 by line 50 has constant characteristics which are highly advantageous.

A further modified embodiment, also, employ ing a moving-bed type of catalytic conversion operation is illustrated in Figure V. In this embodiment, a suitable. feed stock for the process such as a reduced if crude oil is picked up from source 88 by pump BI and passed through heater 82 and line 83 into fractionating column 84 where fractional distillation of the oil is effected. The non-volatile portion, if any, is withdrawn as bottoms through line 85 while the remaining portion is divided into light and heavy fractions which are drawn off through lines 86 and 81 respectively. The light fraction passing overhead through line 86 as a vapor is cooled in exchanger 88; and con.-

densed in condenser 89 and part of the condensate is pumped back from condenser 89 by pump 98 to serve as reflux to column 84. Liquid from condenser 89 is pumped by pump 9| through line 92 through a suitable heater 93 and the resultant vapors passed through line 94 to reactor 95. In reactor 95, conversion of gasoline is effected in the presence of the preconditioned catalyst. If desired, vapors from line 86, may be only partially condensed to supply the required quantity of reflux, and the uncondensed vapors heated to the reaction temperature required in reactor 95. The heavier fraction separated in column 84 is withdrawn by pump 96 and passed through line 81 to heater 98, and thence to heavy oil reactor 99 where conversion into gasoline is effected in the presence of the catalystl and the catalyst is conditioned in accordance with my invention, for use in reactor 95. As in the case of Figure IV, the volatile heavy fraction introduced through line 8! may be replaced by a non-volatile carbogen.

The conversion products from reactors 99 and 95 are withdrawn through lines I88 and Illl respectively and may be suitably fractionated into tail gas, gasoline, recycle stock and tar, in a conventional system of partial condensers or fractionators I82.

Hot regenerated catalyst is carried by a conveyor system I83 and discharged into reactor 99, traveling therethrough from top to bottom and dropping through a star feeder orsolids pump- I into reactor 95. The catalyst continues downwardly through reactor and drops through a star feeder or solids pump I88 into regenerator I8'I wherein the accumulated impurities are removed by burning with air or other suitable regenerating gas introduced through I88. The hot regenerated catalyst is returned to reactor 99 through conveyor system I83, and gaseous regeneration products are withdrawn through duct I89.

From the foregoing it will be apparent that the process therein described accomplishes the object of my invention of providing a process for the catalytic conversion of hydrocarbons whereby a, more favorable distribution and enhanced yield of the desired conversion products is obtained.

It will further be readily apparent to those skilled in the art that while the invention has been illustrated and described with respect to a preferred operation and examples, and with reference to suitable apparatus for its practice, the invention is not limited to such exemplifications but may variously be practiced and embodied within the scope of the claims hereafter made. I

I claim:

1. In a process for catalytically converting high-boiling hydrocarbons into low-boiling hydrocarbons distilling within the gasoline boiling range wherein the cracking catalyst is circulated successively through a conversion zone, and a regeneration zone for burning off carbonaceous deposits formed during the conversion reaction, the improvement comprising separating the hydrocarbon charge into a light fraction and a heavy fraction relatively readily heat decomposable to produce coke or carbon compared to said light fraction, passing the heavy fraction in contact with the hot regenerated catalyst, whereby the heat imparted to the oil by the hot catalyst causes carbon-producing reaction conditions thereby producing a deposit of carbon thereon, and then circulating the catalyst into contact with the light fraction under reacting conditions adapted to produce the required degree of conversion into low-boiling hydrocarbons distilling within the gasoline boiling range.

2. In a process for catalytically converting a petroleum crude into low-boiling hydrocarbons distilling within the gasoline boiling range wherein the cracking catalyst is circulated successively through a conversion zone, and a regeneration zone for burning off carbonaceous-- deposits formed during the conversion reaction, the improvement comprising separating the hydrocarbon charge into a light fraction and a reduced petroleum crude relatively readily heat decomposable to produce coke or carbon compared to said light fraction, passing the reduced crude in contact with the hot regenerated catalyst under carbon-producing reaction conditions thereby producing a deposit of carbon thereon, and then circulating the catalyst into contact with the light fraction under reacting conditions adapted to produce the required degree of conversion into low-boiling hydrocarbons distilling within the gasoline boiling range. V

3. In a process for catalytically converting high-boiling hydrocarbons into low-boiling hydrocarbons distilling within the gasoline boiling range wherein the cracking catalyst is circulated successively through a conversion zone, and a regeneration zone for burning of! carbonaceous deposits formed during the conversion reaction, the improvement comprising first contacting the hot regenerated catalyst with a relatively highboiling hydrocarbon fraction whereby heat is imparted to said oil by said hot catalyst so that a carbonaceous deposit is produced on the catalyst and volatile hydrocarbons are produced, recovering the volatile hydrocarbons thus produced, and passing the catalyst with the carbonaceous deposit thereon into contact with relatively low-boiling volatilized hydrocarbons under conditions effective to produce substantial cracking of said last-mentioned hydrocarbons.

4. In a process for catalytically converting high-boiling hydrocarbons into low-boiling hydrocarbons distilling within the gasoline boiling range wherein the cracking catalyst is circulated successively through a conversion zone, and a regeneration zone for burning ofi carbonaceous deposits formed during the conversion reaction, the improvement comprising first contacting the hot regenerated catalyst with a relatively highboiling reduced crude petroleum oil whereby heat is imparted to said oil by said hot catalyst so that a carbonaceous deposit is produced on the catalyst and volatile hydrocarbons are produced, recovering the volatile hydrocarbons thus produced, and passing the catalyst with the carbonaceous deposit thereon into contact with relatively low-boiling volatilized hydrocarbons under conditions effective to produce substantial cracking of said last-mentioned hydrocarbons.

5. In a process for catalytically converting high-boiling hydrocarbons into low-boiling hydrocarbons distilling within the gasoline boiling range wherein the cracking catalyst is circulated successively through a conversion zone, and a regeneration zone for burning ofi carbonaceous deposits formed during the conversion reaction, the step comprising contacting the hot regen erated catalyst in a contacting zone with a relatively high-boiling reduced crude whereby heat is imparted to said oil by said hot catalyst so that a carbonaceous deposit is produced on the catalyst and volatile hydrocarbons are produced, passing the catalyst with the car-bonaceous deposit thereon i'rom the contacting zone into a cracking zone and into contact with relatively low-boiling volatilized hydrocarbons, and maintaining conditions in said cracking zone effective to produce substantial cracking of said relatively low-boiling volatilized hydrocarbons.

ROBERT F. RUTHRUFF.

REFERENCES CITED- The following references are of record in the file of this patent:

UNITED STATES PATENTS Number Name Date 1,967,636 Towne July 24, 1934 2,253,486 Belchetz Aug. 19, 1941 2,289,329 Prickett July '7, 1942 2,354,546 Reeves July 25, 1944 2,357,136 Rubin Aug. 29, 1944 2,027,552 Roberts Jan, 14, 1936 2,239,801 Voorhees Apr. 29, 1941 2,341,193 Scheineman Feb. 8, 1944 

